EP2531442B1 - Séparation de gaz - Google Patents

Séparation de gaz Download PDF

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Publication number
EP2531442B1
EP2531442B1 EP11701542.0A EP11701542A EP2531442B1 EP 2531442 B1 EP2531442 B1 EP 2531442B1 EP 11701542 A EP11701542 A EP 11701542A EP 2531442 B1 EP2531442 B1 EP 2531442B1
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Prior art keywords
gas
solvent
carbon dioxide
shifted
scrubber
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EP11701542.0A
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German (de)
English (en)
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EP2531442A1 (fr
Inventor
Michael Edward Bailey
Stefano Consonni
Jonathan Alec Forsyth
Manuele Gatti
Emanuele Martelli
Yasushi Moryi
Kazumasa Ogura
Federico Vigano
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BP Technology Ventures Ltd
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BP Technology Ventures Ltd
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Priority claimed from GBGB1001710.1A external-priority patent/GB201001710D0/en
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    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/506—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification at low temperatures
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B3/00—Hydrogen; Gaseous mixtures containing hydrogen; Separation of hydrogen from mixtures containing it; Purification of hydrogen
    • C01B3/50—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification
    • C01B3/52—Separation of hydrogen or hydrogen containing gases from gaseous mixtures, e.g. purification by contacting with liquids; Regeneration of used liquids
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/0605—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the feed stream
    • F25J3/0625—H2/CO mixtures, i.e. synthesis gas; Water gas or shifted synthesis gas
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/0655—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of hydrogen
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J3/00—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification
    • F25J3/06—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation
    • F25J3/063—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream
    • F25J3/067—Processes or apparatus for separating the constituents of gaseous or liquefied gaseous mixtures involving the use of liquefaction or solidification by partial condensation characterised by the separated product stream separation of carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0415—Purification by absorption in liquids
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/046—Purification by cryogenic separation
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0475—Composition of the impurity the impurity being carbon dioxide
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/04—Integrated processes for the production of hydrogen or synthesis gas containing a purification step for the hydrogen or the synthesis gas
    • C01B2203/0465—Composition of the impurity
    • C01B2203/0485—Composition of the impurity the impurity being a sulfur compound
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0805—Methods of heating the process for making hydrogen or synthesis gas
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/08—Methods of heating or cooling
    • C01B2203/0872—Methods of cooling
    • C01B2203/0883—Methods of cooling by indirect heat exchange
    • C—CHEMISTRY; METALLURGY
    • C01—INORGANIC CHEMISTRY
    • C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
    • C01B2203/00—Integrated processes for the production of hydrogen or synthesis gas
    • C01B2203/14—Details of the flowsheet
    • C01B2203/146—At least two purification steps in series
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/40—Processes or apparatus using other separation and/or other processing means using hybrid system, i.e. combining cryogenic and non-cryogenic separation techniques
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2205/00—Processes or apparatus using other separation and/or other processing means
    • F25J2205/50—Processes or apparatus using other separation and/or other processing means using absorption, i.e. with selective solvents or lean oil, heavier CnHm and including generally a regeneration step for the solvent or lean oil
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2215/00—Processes characterised by the type or other details of the product stream
    • F25J2215/04—Recovery of liquid products
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2230/00—Processes or apparatus involving steps for increasing the pressure of gaseous process streams
    • F25J2230/30—Compression of the feed stream
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2240/00—Processes or apparatus involving steps for expanding of process streams
    • F25J2240/30—Dynamic liquid or hydraulic expansion with extraction of work, e.g. single phase or two-phase turbine
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F25—REFRIGERATION OR COOLING; COMBINED HEATING AND REFRIGERATION SYSTEMS; HEAT PUMP SYSTEMS; MANUFACTURE OR STORAGE OF ICE; LIQUEFACTION SOLIDIFICATION OF GASES
    • F25J—LIQUEFACTION, SOLIDIFICATION OR SEPARATION OF GASES OR GASEOUS OR LIQUEFIED GASEOUS MIXTURES BY PRESSURE AND COLD TREATMENT OR BY BRINGING THEM INTO THE SUPERCRITICAL STATE
    • F25J2270/00—Refrigeration techniques used
    • F25J2270/04—Internal refrigeration with work-producing gas expansion loop
    • F25J2270/06—Internal refrigeration with work-producing gas expansion loop with multiple gas expansion loops
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
    • Y02P20/00—Technologies relating to chemical industry
    • Y02P20/151—Reduction of greenhouse gas [GHG] emissions, e.g. CO2

Definitions

  • the present invention relates to a process for separating carbon dioxide from a mixture of gases in which the other main component is hydrogen.
  • the present invention relates to a process where carbon dioxide and hydrogen are separated and recovered as pure streams from sour shifted synthesis gas.
  • the process described comprises in general terms first compressing and cooling the dried shifted product to a pressure and temperature at which carbon dioxide liquefies and thereafter separating the liquid carbon dioxide so generated from the other non-condensable gases (mostly hydrogen). Thereafter the separated components are returned to a temperature and pressure suitable for further use by a plurality of heat exchangers and turbo-expanders integrated amongst themselves and with those used to cool the incoming shifted mixture so that the total energy across the whole process is managed for optimum efficiency.
  • Our application describes process configurations for achieving this outcome and in particular the use of compact, diffusion-bonded multi-channel heat exchangers to reduce the number of heat exchangers needed thereby simplifying the demands on hardware and space. Furthermore by utilising a plurality of turbo-expanders it is possible to carry out the whole process with improved energy efficiency and utilisation by closely matching the cooling curves and characteristics of the various streams employed in the process.
  • shifted gas which is 'sweet' i.e. one which contains minimal levels of 'sour' sulphur containing components such as hydrogen sulphide, sulphur dioxide, carbonyl sulphides and the volatile mercaptans.
  • 'sour' sulphur containing components such as hydrogen sulphide, sulphur dioxide, carbonyl sulphides and the volatile mercaptans.
  • any such components typically end up in the liquid carbon dioxide thereby potentially causing their own environmental concerns if for example the carbon dioxide is stored underground.
  • the initial synthesis gas is 'sour', as is typically the case when the initial carbonaceous feedstock is coal or low grade sources of carbon such as lignite, tar sand or shale oil, further strategies need to be applied to isolate these sulphur-containing components.
  • WO 2010/103259 A2 and EP 2023067 A1 disclose further processes for recovering carbon dioxide and hydrogen from sour shifted synthesis gas. It is now been found that the process described in PCT/GB/2009/02895 can be modified to efficiently treat sour shifted synthesis gas by scrubbing the shifted synthesis gas before the carbon dioxide is liquefied and integrating the operation of this scrubber with the scrubber used to remove carbon dioxide from the hydrogen-containing gas downstream of the gas liquid separator.
  • a process for separating a sour shifted synthesis gas feedstock into liquid carbon dioxide, a gaseous hydrogen-containing gas and separated sulphur-containing components by superatmospheric refrigeration characterised in that the process comprises the following stages:
  • the present invention has the advantage that by integrating the two scrubbers so that they utilize a common solvent greater energy efficiency is achieved relative to previously described processes.
  • the need to vapourised and re-condense the carbon dioxide is obviated thereby simplifying the process considerably given the volume of liquid carbon dioxide concerned.
  • stage (a) of the process of the present invention sour shifted synthesis gas typically at a pressure in the range 50 to 250 bar is fed to a first scrubber, typically a column, where it is contacted with an alcohol solvent.
  • this alcohol solvent is derived from the second scrubber of stage (d) and contains dissolved carbon dioxide.
  • Stage (a) is typically effected by continuously contacting a stream of the sour shifted gas with a stream of the cold alcohol under conditions which cause intimate and turbulent mixing of the two for example by counter-current mixing or by sparging the shifted gas through the alcohol. Under these conditions the sulphur-containing components and some of the carbon dioxide in the shifted gas dissolve in the alcohol and are removed from the system by way of an outlet effluent stream.
  • this temperature gradient is defined by an inlet temperature of the cold alcohol in the range -50 to 0°C most preferably -50 to -20°C and an outlet temperature of the warmed alcohol suitably in the range 0 to 50°C preferably +5 to +35°C.
  • inlet and outlet temperatures will depend upon the gas and solvent flow rates used and to a certain extent by how much carbon dioxide can be tolerated in the effluent stream.
  • outlet temperature should be chosen so that essentially all of the sulphur-containing components are removed by the first scrubber.
  • sweet shift gas is then removed overhead from the column and the outlet alcohol stream now containing both dissolved carbon dioxide and the sulphur-containing components removed from the bottom.
  • the outlet effluent stream so removed is then fed to at least one, preferably a series of flash vessels where the pressure is partially let down allowing carbon dioxide to be released from the alcohol solvent whilst the sulphur-containing components remain dissolved therein.
  • this stream is fed to at least one, preferably a series of heat exchangers and separators where the temperature is gradually increased allowing carbon dioxide to be released from the alcohol solvent whilst the sulphur-containing components remain dissolved therein.
  • the alcohol solvent now essentially containing essentially only dissolved sulphur-containing components is then removed and fed to a stripper column which regenerates pure alcohol and a gaseous stream of the sulphur-containing components which can be further processed in for example a Claus plant to recover the sulphur in elemental form.
  • the carbon dioxide released by the flash vessels can be collected, combined and fed back into the system. This feeding back can occur at a number of points including (1) into the sour shifted synthesis gas feed to stage (a), (2) into the second scrubber or the alcohol stream being fed thereto (stage (d)) or (3) into the sweetened shifted synthesis gas exiting the first scrubber. Of these possibilities the first is generally the most preferred.
  • the sweet shift gas at a pressure in the range 50 to 250 bar is optionally further compressed and then cooled until some preferably over 90% of the carbon dioxide contained therein liquefies.
  • this involves passing the shifted gas though at least one heat exchanger in which it enters into heat exchange relationship with the cold separated liquid carbon dioxide and/or hydrogen rich fractions generated in stage (c) below thereby allowing these latter fractions to be warmed back towards their final desired temperature.
  • the flows of the shifted gas, the cold separated liquid carbon dioxide and the hydrogen rich fractions are configured so as to flow though at least one or at least one array of multi-channel diffusion bonded and/or micro-channel heat exchangers thereby cooling the shifted gas mixture to the operating temperature of the fractionation unit.
  • heat exchangers are described for example in EP 0212878 and WO 2004/017008 .
  • stage (c) the cooled shifted gas (now a two-phase mixture of liquid carbon dioxide and a non-condensable hydrogen rich gas) is separated in a fractionation unit.
  • thermodynamic constraints referred to above relate to ideal systems and that the shifted gases being treated herein may exhibit significant deviation from ideality potentially giving rise to an elevation of the triple point temperature.
  • the temperature of the fractionation unit should be at least 3°C preferably at least 5°C above the theoretical triple point temperature of carbon dioxide. In practical terms and for the mixtures described herein this generally means operating the fractionation unit at a temperature in the range -25 to -53°C and preferably in the range -40 to -50°C.
  • the pressure should preferably be in the range 50 to 250 bar, preferably 100 to 200 bar as mentioned above.
  • the fractionation unit used in the process of the present invention is for example a conventional gas-liquid separator adapted to work at the high pressures and low temperatures set out above. In such vessels the gaseous hydrogen rich fraction is typically taken off overhead and the liquid carbon dioxide removed at or near the bottom.
  • the pressure drop across the fractionator is typically no more than between 0.1 and 0.5bar.
  • the separation of liquid carbon is carried out in a series of fractionating units at the same pressure and different temperatures or most preferably at the same temperature and different pressures.
  • a first fractionation unit might operate at a temperature in the range -20 to -53°C and at a pressure in the range 50 to 100bar and the second fractionation unit at a temperature in the same range but at a pressure in the range 100 to 200bar.
  • the second fractionation unit at a temperature in the same range but at a pressure in the range 100 to 200bar.
  • An advantage of this approach it reduces the amount of gas which needs to be compressed to very high pressures.
  • the gaseous hydrogen-rich fraction is in stage (d) fed to a second scrubber where it is contacted with preferably a continuously fed and continuously removed stream of cold alcohol in order to extract residual carbon dioxide therefrom.
  • a second scrubber where it is contacted with preferably a continuously fed and continuously removed stream of cold alcohol in order to extract residual carbon dioxide therefrom.
  • This is typically effected by continuously contacting the hydrogen-rich fraction with the cold alcohol stream in a column under conditions which cause intimate and turbulent mixing of the two for example by counter-current mixing or by sparging the hydrogen rich fraction through the solvent. Under these conditions the residual carbon dioxide dissolves in the alcohol and is removed from the system by way of an effluent stream from the second scrubber.
  • thermodynamic driving force behind this absorption process works synergistically with the increased capacity of the solvent at low temperature to hold proportionately more carbon dioxide making a highly efficient system.
  • it is more efficient than the alternative i.e. conventional use of a Rectisol or Selexol treatment carried out at much lower pressures after the hydrogen-rich fraction has been returned to or near to its final desired state.
  • the alcohol solvent used is selected from methanol, ethanol, the isomers of propanol and low molecular weight glycols and glycol ethers formed by oligomerisation of ethylene or propylene glycol.
  • the alcohol solvent chosen should be one which will not freeze under the operating conditions of either the first or second scrubbers. Since it is preferred that this second scrubbing is conducted immediately after stage (c) with no intermediate treatment of the hydrogen-rich fraction the operating temperature and pressure of the second scrubber should be the same as or substantially the same as those of the final fractionation unit.
  • stage (e) of the process the effluent alcohol solvent from the second scrubber now containing dissolved carbon dioxide is next fed to the first scrubber of stage (a).
  • the alcohol solvent may optionally be passed through a heat exchanger to warm or cool it as they case may be depending on the relative operating conditions of the two scrubbers. Whilst it is preferred that the two scrubbers are operated isobarically if the first scrubber is operated at a higher pressure than the second it may be necessary to pump the effluent solvent between the two.
  • stage (f) of the process of the present invention the hydrogen-rich fraction exiting stage (d) is warmed and decompressed in order to restore it to the temperature and pressure required for its further utilisation.
  • this stage is effected by passing this fraction through one preferably a plurality of turbo-expanders and associated interstage heat exchangers arranged in series.
  • each turbo-expander the hydrogen-rich fraction is expanded isentropically progressively reducing its pressure and progressively releasing expansion energy which in turn drives a turbine capable of recovering this energy as mechanical work.
  • the process of the present invention may suitably employ from two to eight turbo-expanders arranged in series preferably from two to six.
  • the turbo-expanders themselves are conveniently arranged so that they drive a common shaft.
  • the mechanical work generated can if desired be used elsewhere in the process thereby minimizing overall energy usage.
  • the expansion of the hydrogen-rich fraction causes it to cool and the cooling capacity generated can be recovered in interstage heat exchangers and used to cool warmer streams elsewhere in the system especially those involved in stage (b).
  • these interstage coolers are integrated into a single or array of multi-channel heat exchangers though which the incoming sweetened shifted gas of stage (b) also flows in order to manage the cooling capacity of the whole system as efficiently as possible.
  • stage (b) also flows in order to manage the cooling capacity of the whole system as efficiently as possible.
  • liquid carbon dioxide recovered in stage (c) will depend to a certain extent on what is to be done with it. It may for example be piped or tankered offsite for underground storage. In this case it is desirable to liquefy any further gaseous carbon dioxide recovered in the optional scrubbing stage and combine it with the material recovered in stage (c).
  • the liquid carbon dioxide may if desired be warmed by passing it through the multichannel heat exchanger to utilize its cooling capacity too. It is preferred that little or no expansion of the liquid carbon dioxide occurs downstream of the fractionation unit so that its pressure is maintained at or above 50 bar after the fractionation unit.
  • shifted syngas exiting the H 2 S absorber or first scrubber may contain significant amounts of the alcohol solvent (for example methanol) from the absorber.
  • the alcohol solvent for example methanol
  • the process of the present invention may further include the step of recovering solvent from the sweet shifted gas generated in step (a).
  • the step of recovering solvent may for example include cooling the sweet shifted gas generated in step (a), and separating solvent from the cooled sweet shifted gas.
  • the method may further include and feeding the separated solvent to a scrubber.
  • the separated solvent may be fed to the first scrubber.
  • the separated solvent may be fed to another solvent system used in the process, for example a second scrubber.
  • the solvent may be exported from the system.
  • the gas leaving the absorber may be cooled to condense solvent in the gas.
  • the gas may be cooled using a heat exchanger system, for example including a coolant or refrigerant which may include an internal process stream and/or an external stream.
  • a heat exchanger system for example including a coolant or refrigerant which may include an internal process stream and/or an external stream.
  • the gas leaving the absorber may be cooled by expansion of the gas.
  • the recovery of the solvent may be effected through an expansion and separation method.
  • the process of the present invention may further include the step of passing gas leaving an absorber to an expander, and expanding the gas to form a cooled gas and solvent liquid, and separating the solvent from the cooled gas.
  • the process may further include the step of compressing the cooled gas after the separation of the solvent.
  • the energy for the compression step may be provided by work recovered in the expansion step.
  • the cooled gas may be compressed back to its original pressure.
  • the gas may be for example expanded to less than 40Bar, for example 30Bar or less, for example 25 bar.
  • the gas is expanded to a pressure above 20Bar to reduce the likelihood of significant CO 2 condensation.
  • an expander may be provided downstream of the first scrubber A1.
  • the expander may reduce the pressure of the gas to 25 bar and the temperature to - 8 °C. After separation of methanol solvent from the stream, it has been found in some examples that approximately 0.12 mol% methanol remained in the shifted synthesis gas. This represents less than one tenth of the amount of methanol leaving the absorber at a pressure of 60 bar (see above).
  • more than one method may be used to cool the gas stream to condense solvent, and the different methods may be used in any appropriate order.
  • the gas exiting the intermediate separator after separation of condensed solvent may be warmed and washed with water in a suitably designed contactor.
  • the resulting gas stream will contain a reduced amount of solvent and may be in some cases substantially free of solvent (for example methanol) and saturated with water.
  • the water is then preferably removed from the substantially solvent free gas, for example by a standard drying method.
  • the solvent for example methanol, may be recovered from the solvent-containing water stream exiting the wash column by distillation, wherein the purified water may then be returned to the water wash column.
  • the substantially dried solvent may be returned back to the solvent system.
  • a cooling and condensing step would usually be carried out to remove some of the solvent from the gas before a water washing procedure is carried out, but it is envisaged that the water washing might be carried out before, or instead of, a cooling and condensing separation procedure.
  • a solvent other than water might be used to wash the solvent from the gas.
  • features relating to the removal of solvent, for example alcohol solvent, for example methanol, from the gas may be applied to other processes.
  • features relating to the removal of solvent from the gas may be applied to other methods in which a gas including carbon dioxide includes an alcohol solvent to be removed.
  • a gas separation plant for converting sour shifted synthesis gas into separate streams consisting of liquid carbon dioxide, a hydrogen-rich fraction and sulphur-containing components according to a process of the invention which comprises;
  • the shift and separation plant described above may typically form part of a larger integrated complex for example an Integrated Gasification Combined Cycle (IGCC) or similar hydrogen power plants which include the additional step of burning the hydrogen (preferably diluted with nitrogen) in the burners of a gas turbine.
  • IGCC Integrated Gasification Combined Cycle
  • some or all of the hydrogen so generated can be used in various refinery applications such as hydrocracking and hydrotreating.
  • the plant may further include a solvent recovery system including means for cooling a gas including solvent, and a separator.
  • the means for cooling the gas may include an expander, the expander preferably being arranged to receive and expand a gas including solvent to form a gas including liquid solvent, the separator being arranged to separate the liquid solvent from the gas.
  • a high temperature sour shifted synthesis gas feedstock at a pressure of 60 bar is fed via line 2 to a heat exchanger E1 where it is cooled to a temperature of 9°C before being fed via 3 to a first scrubber A1 where it is contacted with a methanol solvent containing dissolved carbon dioxide.
  • the methanol solvent used is obtained from a second scrubber A3 (see below), fed to the top of A1 via 13 and removed from the bottom via 4.
  • the methanol is warmed by the sour shifted synthesis gas from an inlet temperature of -50°C to an outlet temperature of approximately +12°C.
  • methanol solvent from F3 still containing dissolved sulphur-containing components is fed via 10 to a heat exchanger E2 where it is warmed prior to being fed to a stripper A2 in which the sulphur-containing components are separated and removed overhead via 11 before being sent for further processing in a Claus plant. Any final amounts of carbon dioxide present in the stream to the Claus plant may be recovered as a tail gas for recycling to line 2 as well (not shown). Pure methanol is removed from the bottom of A2 via line 12 after which it is fed via 24 to the top of A3 after having been cooled in a heat exchanger E3 and topped up with fresh methanol as required.
  • Sweet shifted synthesis gas at 60 bar is removed overhead from A1 via 14 after which it is cooled in one or a series of heat exchanger (shown schematically in Figure 1 as E4) to -50°C in order to create a two-phase mixture of liquid carbon dioxide and a hydrogen-containing gas.
  • the two-phase mixture is next fed via 15 to a first fractionator F4 where it is separated into liquid carbon dioxide and residual gas. Thereafter the liquid is taken off at the bottom via 16 whilst the gas is taken off overhead via 17, compressed and cooled in one or more compressors and associated heat exchanger (shown schematically in Figure 1 as C4 and E5) to a pressure of 150 bar and -50°C creating a second two-phase mixture which is separated in a second separator F5 as before.
  • the liquid carbon dioxide obtained from F5 is fed via 18 to 16 where it is combined with that recovered from F4 before being taken away for storage.
  • the various heat exchangers used in this stage are integrated with cold streams in the turbo-expander/heat exchanger section described below in order to utilize the cooling capacity of these latter streams.
  • the gas recovered overhead from F5 now rich in hydrogen and at a pressure of 150 bar and -50°C is next fed via 19 to the base of A3 where it is contacted countercurrently with cold methanol at the same temperature.
  • the cold methanol is warmed and extracts residual carbon dioxide from the hydrogen containing gas prior to the treated gas being removed overhead via line 20.
  • the methanol containing dissolved carbon dioxide is removed from the bottom of A3 via 21 at a temperature of - -35°C reduced in pressure to 60 bar by means of a hydraulic turbine T1 before being fed first to a separator A5 to remove and recycle any entrained hydrogen (via line 22) and then cooled in heat exchanger E6 back down to -50°C before being fed via 13 to A1.
  • the hydrogen gas removed overhead from A3 still at a pressure of 150 bar and -50°C is warmed in heat exchanger E7 and progressively reduced in pressure and warmed by a series of turbo-expanders T2, T3 and T4 and associated interstage heat exchangers E8, E9 and 10 to near ambient temperature and a pressure of 30bar. In doing so the energy released by the turbo-expanders is used to generate power for driving other equipment.
  • the cooling capacity removed in E7 and in E8, E9 and E10 (caused by expansion of the hydrogen-containing gas) is used to supply cooling capacity to the heat exchangers E4 and E5.
  • the hydrogen-containing gas leaving the final heat exchanger via line 23 can optionally be fed to the burners of one or more gas turbines (not shown) where the hydrogen is burnt with an oxygen containing gas to generate power and steam.
  • Figure 2 illustrates a variant on the scheme shown in Figure 1 incorporating two other features. These are (1) the first and second scrubbers work under the same high pressure and (2) the carbon dioxide is released from the first scrubber alcohol effluent stream by means of a progressive temperature rise through a series of heat exchangers.
  • a high temperature sour shifted synthesis gas feedstock at a pressure of 60 bar fed via line 2 is compressed and cooled in one or more compressors and associated heat exchangers (shown schematically in Figure 2 as C4 and E1) to a pressure of 150 bar.
  • Heat exchanger E1 then cools the synthesis gas down to a temperature of 9°C before it is fed via 3 to a first scrubber A1 where it is contacted with a methanol solvent containing dissolved carbon dioxide as described above in Example 1.
  • the methanol solvent used is obtained from a second scrubber A3 (see below), fed to the top of A1 via 13 and removed from the bottom via 4.
  • the methanol so removed and now containing the sulphur-containing components and some carbon dioxide is fed then via 4, 5 and 6 to a series of heat exchangers and separators (E11,E12,E13, F1 and F2) where the temperature is progressively increased and carbon dioxide is released.
  • Overhead gas streams 7 and 8 from each of F2 and F1 are fed to heat exchangers E12 and E11 arranged in series which recover heat for heating up the incoming stream and then recycled via 25 to line 2.
  • E13 supplements heat required for these heat exchange process.
  • the methanol solvent from F2 still containing dissolved sulphur-containing components is reduced in pressure by means of a hydraulic turbine T1 before being fed via 10 to a heat exchanger E2 where it is optionally warmed prior to being fed to a stripper A2 in which the sulphur-containing components are separated and removed overhead via 11 before being sent for further processing in a Claus plant.
  • Pure methanol is removed from the bottom of A2 via line 12 after which it is fed via 24 to the top of A3 after having been cooled in a heat exchanger E3 and topped up with fresh methanol as required.
  • Sweet shifted synthesis gas at 150 bar is removed overhead from A1 via 14 after which it is cooled in one or a series of heat exchanger (shown schematically in Figure 1 as E4) to -30°C in order to create a two-phase mixture of liquid carbon dioxide and a hydrogen-containing gas.
  • the two-phase mixture is next fed via 15 to a first fractionator F4 where it is separated into liquid carbon dioxide and residual gas. Thereafter the liquid is taken off at the bottom via 16 whilst the gas is taken off overhead via 17, cooled in one or more heat exchanger (shown schematically in Figure 2 as E5) to -50°C creating a second two-phase mixture which is separated in a second separator F5 as before.
  • the liquid carbon dioxide obtained from F5 is fed via 18 to 16 where it is combined with that recovered from F4 before being taken away for storage.
  • the various heat exchangers used in this stage are integrated with cold streams in the turbo-expander/heat exchanger section described below in order to utilize the cooling capacity of these latter streams.
  • the gas recovered overhead from F5 now rich in hydrogen and at a pressure of 150 bar and -50°C is next fed via 19 to the base of A3 where it is contacted countercurrently with cold methanol at the same temperature.
  • the cold methanol extracts residual carbon dioxide from the hydrogen containing gas prior to the treated gas being removed overhead via line 20. Meanwhile the methanol containing dissolved carbon dioxide is removed from the bottom of A3 via 21 and optionally cooled in heat exchanger E6 before being fed via 13 to A1.
  • the hydrogen gas removed overhead from A3 still at a pressure of 150 bar and -50°C is warmed in heat exchanger E7 and progressively reduced in pressure and warmed by a series of turbo-expanders T2, T3 and T4 and associated interstage heat exchangers E8, E9 and 10 to near ambient temperature and a pressure of 30bar. In doing so the energy released by the turbo-expanders is used to generate power for driving other equipment.
  • the cooling capacity removed in E7 and in E8, E9 and E10 (caused by expansion of the hydrogen-containing gas) is used to supply cooling capacity to the heat exchangers E4 and E5.
  • the hydrogen-containing gas leaving the final heat exchanger via line 23 can optionally be fed to the burners of one or more gas turbines (not shown) where the hydrogen is burnt with an oxygen containing gas to generate power and steam.
  • Figure 3 illustrates a variant on the scheme shown in Figure 2 incorporating a methanol recovery feature provided by the separator Fx and heat exchanger Ex. Using these additional features, methanol is recovered and returned to the top tray of the H 2 S absorber.
  • a high temperature sour shifted synthesis gas feedstock at a pressure of 60 bar fed via line 2 is compressed and cooled in one or more compressors and associated heat exchangers as described in relation to Figure 2 to a pressure of 150 bar.
  • Heat exchanger E1 then cools the synthesis gas down before it is fed via 3 to a first scrubber A1 where it is contacted with a methanol solvent containing dissolved carbon dioxide as described above in Example 1.
  • the methanol solvent used is obtained from a second scrubber A3 (see below), fed to the top of A1 via 13 and removed from the bottom via 4.
  • the methanol so removed and now containing the sulphur-containing components and some carbon dioxide is fed then via 4, 5 and 6 to a series of heat exchangers and separators (E11,E12,E13, F1 and F2) as described in relation to Figure 2 in which the sulphur-containing components are separated and removed before being sent for further processing in a Claus plant.
  • Pure methanol is removed from the bottom of A2 via line 12 after which it is fed via 24 to the top of A3 after having been cooled in a heat exchanger E3 and topped up with fresh methanol as required.
  • Sweet shifted synthesis gas at 150 bar is removed overhead from A1 via 14.
  • an initial intermediate cooling is carried out in heat exchanger system Ex (which may include one or more heat exchanger elements) to cool the gas to a temperature of about 13 degrees C.
  • the cooled gas is passed to an intermediate separator from which methanol is removed and passed back to the first scrubber A1.
  • the treated shifted syngas is then passed to the heat exchanger system E4 for subsequent process steps as described in relation to Figure 2 .
  • Example 3 Other features of Example 3 are as described in relation to Figure 2 .
  • the recovery of methanol from the process can be for example more than 90%, for example 94%.
  • heat exchanger Ex could be replaced by an expander which would effect cooling of the gas stream by expansion.
  • a compressor may be provided upstream of heat exchanger E4 to repressurise the gas stream after separation of the solvent.
  • a water washing apparatus may be provided downstream of the separator Fx to remove further methanol from the gas.
  • a contactor may be provided downstream of the separator Fx to wash the gas with water.
  • the resulting gas stream will contain a reduced amount of solvent and may be in some cases substantially free of solvent (for example methanol) and saturated with water.
  • the water is then preferably removed from the substantially solvent free gas, for example by a standard drying method.
  • the solvent for example methanol, may be recovered from the solvent-containing water stream exiting the wash column by distillation, wherein the purified water may then be returned to the water wash column.
  • the substantially dried solvent may be returned back to the solvent system.

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Claims (15)

  1. Procédé de séparation d'une matière première de gaz de synthèse décalé acide en du dioxyde de carbone liquide, un gaz contenant de l'hydrogène gazeux et des composants contenant du soufre séparés par réfrigération superatmosphérique dans lequel le procédé comprend les étapes suivantes :
    a. épurer le gaz décalé acide à pression élevée avec un solvant alcoolique dans un premier épurateur et récupérer séparément un courant d'alcool contenant les composants contenant du soufre et un gaz décalé doux ;
    b. ensuite refroidir le gaz décalé doux à une température et une pression élevée auxquelles le dioxyde de carbone contenu dans celui-ci se condense et un mélange liquide de gaz à deux phases est formé ;
    c. séparer le mélange à deux phases de l'étape (b) en une fraction séparée de dioxyde de carbone liquide et une fraction contenant de l'hydrogène gazeux dans une unité de fractionnement ;
    d. extraire du dioxyde de carbone résiduel de la fraction séparée contenant de l'hydrogène gazeux en épurant la fraction contenant de l'hydrogène gazeux à pression élevée avec un solvant alcoolique dans un deuxième épurateur et récupérer un courant d'alcool contenant du dioxyde de carbone ;
    e. alimenter le premier épurateur avec le courant d'alcool contenant du dioxyde de carbone produit dans l'étape (d) et
    f. chauffer et détendre la fraction contenant de l'hydrogène gazeux épurée en utilisant au moins un échangeur de chaleur pour échanger de la chaleur avec le mélange de l'étape (b) et au moins un turbo-détendeur capable de récupérer du travail mécanique.
  2. Procédé tel que revendiqué dans la revendication 1 caractérisé en ce que le gaz décalé doux est en outre comprimé avant l'étape (b).
  3. Procédé tel que revendiqué dans la revendication 1 caractérisé en ce que le courant d'alcool contenant les composants contenant du soufre est traité pour récupérer tout dioxyde de carbone dissous dans celui-ci.
  4. Procédé tel que revendiqué dans la revendication 3 caractérisé en ce que le dioxyde de carbone est récupéré à travers une série de vaisseaux flash dans lesquels la pression est partiellement abaissée, ou en ce que le dioxyde de carbone est récupéré à travers une série d'échangeurs de chaleur et de séparateurs dans lesquels la température est graduellement augmentée.
  5. Procédé tel que revendiqué dans la revendication 3 caractérisé en ce que le dioxyde de carbone récupéré est recyclé vers la matière première de gaz de synthèse décalé acide, ou alimente le deuxième épurateur, ou est renvoyé au gaz décalé doux.
  6. Procédé tel que revendiqué dans la revendication 1 caractérisé en ce que l'étape (d) emploie une pluralité d'unités de fractionnement fonctionnant à la même température mais à des pressions différentes.
  7. Procédé tel que revendiqué dans la revendication 1 caractérisé en ce que la température d'entrée pour le solvant alcoolique dans le premier épurateur est dans la plage de -50 à -20°C et la température de sortie est dans la plage de +5 à +35°C.
  8. Procédé tel que revendiqué dans l'une quelconque des revendications précédentes incluant en outre l'étape de récupération de solvant à partir du gaz décalé doux généré dans l'étape (a), et préférablement de refroidissement du gaz décalé doux généré dans l'étape (a), de séparation du solvant du gaz décalé doux refroidi et d'administration du solvant séparé au premier épurateur.
  9. Procédé selon la revendication 8, incluant faire passer le gaz décalé doux généré dans l'étape (a) dans un détendeur, et détendre le gaz pour former un gaz refroidi et un liquide solvant, et séparer le solvant du gaz refroidi.
  10. Procédé selon la revendication 9, incluant en outre administrer le solvant séparé à un épurateur.
  11. Procédé selon la revendication 9 ou la revendication 10 incluant en outre compresser le gaz refroidi après séparation du solvant du gaz refroidi.
  12. Procédé selon l'une quelconque des revendications 8 à 11 incluant en outre l'étape de lavage du gaz de synthèse décalé doux à l'eau pour enlever du solvant du gaz de synthèse décalé doux, et facultativement incluant en outre l'étape de séchage du gaz de synthèse après l'étape de lavage à l'eau.
  13. Procédé selon la revendication 12, incluant en outre traiter l'eau utilisée pour le lavage après l'étape de lavage pour récupérer du solvant de l'eau, et facultativement incluant administrer le solvant récupéré à un épurateur.
  14. Centrale de séparation de gaz pour convertir du gaz de synthèse décalé acide en des courants séparés consistant en du dioxyde de carbone liquide, une fraction riche en hydrogène et des composants contenant du soufre selon un procédé selon l'une quelconque des revendications 1 à 13, la centrale comprenant :
    a. un premier épurateur pour adoucir un gaz décalé acide en enlevant des composants contenant du soufre pour former un gaz de synthèse décalé adouci ;
    b. un système de refroidissement pour refroidir le gaz décalé adouci à une température à laquelle le dioxyde de carbone se condense et un mélange liquide de gaz à deux phases est formé ledit système de refroidissement comprenant en outre au moins un échangeur de chaleur pour refroidir un gaz de synthèse décalé ;
    c. une unité de fractionnement pour séparer le mélange à deux phases généré dans ledit système de refroidissement en une fraction séparée de dioxyde de carbone liquide et une fraction riche en hydrogène gazeux, la centrale incluant un moyen pour faire passer une fraction liquide de dioxyde de carbone et/ou une fraction riche en hydrogène gazeux de l'unité de fractionnement au système de refroidissement pour un refroidissement contre le gaz de synthèse décalé
    d. un deuxième épurateur pour retirer du dioxyde de carbone résiduel de ladite fraction riche en hydrogène gazeux par extraction en utilisant un solvant alcoolique, la centrale comprenant un moyen pour faire passer un solvant du deuxième épurateur au premier épurateur
    e. un système de détendeur pour réchauffer et détendre la fraction séparée riche en hydrogène gazeux comprenant au moins un turbo-détendeur pour récupérer progressivement de l'énergie à partir de la fraction riche en hydrogène gazeux en tant que travail mécanique et au moins un moyen pour fournir une capacité de refroidissement à au moins un des échangeurs de chaleur dans le système de refroidissement.
  15. Centrale selon la revendication 14, incluant en outre un système de récupération de solvant incluant un moyen pour refroidir un gaz incluant un solvant, et un séparateur, préférablement dans laquelle le moyen pour refroidir le gaz inclut un détendeur, le détendeur étant arrangé pour recevoir et détendre un gaz incluant un solvant pour former un gaz incluant un solvant liquide, le séparateur étant arrangé pour séparer le solvant liquide du gaz.
EP11701542.0A 2010-02-02 2011-01-21 Séparation de gaz Active EP2531442B1 (fr)

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GBGB1001710.1A GB201001710D0 (en) 2010-02-02 2010-02-02 Separation of gases
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EP11701542.0A EP2531442B1 (fr) 2010-02-02 2011-01-21 Séparation de gaz
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DE102012110520B4 (de) * 2012-11-02 2019-01-31 L'Air Liquide Société Anonyme pour l'Etude et l'Exploitation des Procédés Georges Claude Verfahren zur Herstellung von trockenem synthetischem Erdgas (SNG)
CN104208978B (zh) * 2014-08-28 2016-06-29 崔静思 一种气体净化的设备及方法
US20190168175A1 (en) * 2017-12-06 2019-06-06 Larry Baxter Solids-Producing Siphoning Exchanger

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US3614872A (en) 1967-12-22 1971-10-26 Texaco Inc Synthesis gas separation process
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WO2006037320A1 (fr) * 2004-10-08 2006-04-13 Union Engineering A/S Procede de recuperation de dioxyde de carbone a partir d'un gaz
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EP2023067A1 (fr) 2007-07-25 2009-02-11 BP Alternative Energy Holdings Limited Séparation de dioxyde de carbone et d'hydrogène
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WO2011095759A1 (fr) 2011-08-11
EP2531442A1 (fr) 2012-12-12
CN102971253B (zh) 2015-06-17
US9212061B2 (en) 2015-12-15
CN102971253A (zh) 2013-03-13

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